EP2170494B1 - Réacteur en vue de la réalisation d'une réaction triphasique entre une phase liquide et une phase gazeuse sur un lit fixe de catalyseur - Google Patents

Réacteur en vue de la réalisation d'une réaction triphasique entre une phase liquide et une phase gazeuse sur un lit fixe de catalyseur Download PDF

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Publication number
EP2170494B1
EP2170494B1 EP08774160A EP08774160A EP2170494B1 EP 2170494 B1 EP2170494 B1 EP 2170494B1 EP 08774160 A EP08774160 A EP 08774160A EP 08774160 A EP08774160 A EP 08774160A EP 2170494 B1 EP2170494 B1 EP 2170494B1
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European Patent Office
Prior art keywords
reactor
openings
distributor plate
distributor
liquid phase
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EP08774160A
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German (de)
English (en)
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EP2170494A1 (fr
Inventor
Marcus Bechtel
Benjamin Hepfer
Michael Hyatt Regency Xian WILLE
Andreas Daiss
Reiner Geier
Stefan Iselborn
John Sauter
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BASF SE
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BASF SE
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
    • C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
    • C07C7/167—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00548—Flow
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • the invention relates to a reactor for carrying out a three-phase reaction of a liquid and a gaseous phase on a fixed catalyst bed with a mixing and distribution device for the liquid and the gaseous phase, a method for carrying out three-phase reactions and a use.
  • three-phase reactors are usually operated adiabatically, ie the temperature changes as the conversion progresses as a result of the released or absorbed reaction heat, which correspondingly rises or falls in the absence of external heat exchange.
  • a uniform distribution of the reactants is also desirable.
  • the US 5,817,901 describes a process for the selective hydrogenation of hydrocarbon cuts having 2 to 20 carbon atoms per molecule on a fixed bed catalyst, wherein the hydrocarbon stream and hydrogen are passed to the fixed bed via a static mixer type SMV or SMX Sulzer, before which advantageously arranged a not described liquid distributor is.
  • a static mixer type SMV or SMX Sulzer for the selective hydrogenation of butadiene to 1-butenes from a C4 cut for described a reactor with a diameter of 10 cm, with selectivities for the above reaction of butadiene to 1-butenes of not more than about 58% are achieved.
  • the EP-A 1 147 809 describes a distributor for a polyphasic mixture comprising at least one gaseous and at least one liquid phase, on a fixed bed, formed of a distributor plate, are arranged on the drainage tubes, and at the lower end of another distributor element is provided in the form of a sieve.
  • the WO-A 03/039733 describes a distributor for a mixture comprising at least one gaseous and at least one liquid phase, on a fixed bed.
  • the distributor comprises a distributor plate P, on which with a plurality of mixing and drainage tubes through the plate, which has an upper inlet opening for the gas, lateral inlet openings for the liquid and optionally a small part of the gaseous phase and a lower opening for the mixture gaseous and liquid phase, wherein below the lower opening and above a fixed catalyst bed, an additional distributor element in the form of a sieve with controlled porosity and upturned side walls is arranged.
  • the arrangement of the additional distributor element ensures a more uniform loading of the gaseous and liquid phase fixed catalyst bed in comparison to an embodiment without the same.
  • the WO-A 95/35159 describes another two-phase distributor for a gaseous and a liquid phase on a fixed bed with a distributor plate and drain tubes, wherein two groups of drain tubes are provided with openings at different levels, such that a uniform distribution is ensured even at low flow rates.
  • the DE-A 10 2004 021 128 describes a further reactor with supply of a gaseous and a liquid starting material in cocurrent to a fixed-bed catalyst, wherein before the same a distributor plate is provided which has openings with static mixers arranged in the openings.
  • the combination of distributor tray and static mixers allows a significant reduction in the degree of slimming h / d, ie the ratio between height and diameter of the reactor, to values of ⁇ 5.
  • the object is achieved by a reactor according to claim 1.
  • a mixing and distribution device for a liquid and a gaseous phase which comprises two main parts, a liquid phase pre-distributor which is equipped with trough-shaped channels analogously to known trough distributors to which liquid phase drainage tubes are attached but with the peculiarity that the drainpipes extend as far as close to the bottom of the distributor plate, which acts as the main distributor, that the drainpipes always immerse themselves in the liquid that is placed on the distributor base.
  • vertical spouts are introduced in the distributor base, with one or more openings for the entry of the gaseous phase and one or more openings arranged below thereof for the entry of the liquid phase, wherein the number and size of the openings for the entry of the liquid phase are designed in that, for a given liquid feed, the liquid level on the distributor bottom below the openings for the entry of the gaseous phase and above the openings for the entry of the liquid phase.
  • the drainpipes of the predistributor the liquid always enough to below the liquid level on the functioning as the main distributor tray, the liquid draining via the drain tubes from the serving as pre-distributor trough distributor liquid is uniformly introduced into the standing on the distributor bottom liquid without liquid emerges as a jet or even injected.
  • the number and the size of the openings for the entry of the liquid phase into the spouts of the distributor plate are designed such that the liquid level on the distributor tray is up to 20% higher and up to 50%, even if the liquid feed deviates from the given liquid supply % down, below the gaseous phase inlet openings and above the liquid phase inlet openings.
  • a uniform distribution of liquid and gaseous phase is ensured in particular also for large reactors with a diameter in the range of 0.5 to 5 m or in a range of 1 to 4 m, or even in a range of 1.2 to 3 m ,
  • the distributor tray which acts as a main distributor, 50 to 200, or preferably 70 to 150, or even 90 to 130 spouts per m 2 are regularly arranged.
  • the spouts can be aligned in a triangular pitch or in a square graduation on the distributor base.
  • the spouts have a free diameter of 5 to 75 mm, a length of 100 to 600 mm above the distributor plate and a length of 20 to 250 mm below the distributor plate and have openings for the entry of the liquid phase with a diameter of 2 to 45 mm, which are arranged at a height of 10 to 100 mm above the distributor base, and openings for the entry of the gaseous phase with a diameter of 1 to 30 mm.
  • the spouts have a free diameter of 10 to 60 mm, a length of 200 to 400 mm above the distributor bottom and a length of 50 to 200 mm below the distributor bottom, as well as openings for the entry of the liquid phase with a diameter of 3 up to 35 mm at a height of 22 to 75 mm above the distributor bottom and openings for entry of the gaseous phase with a diameter of 5 to 20 mm.
  • the spouts have a free diameter of 35 to 50 mm, a length of 250 to 350 mm above the distributor tray and a length of 100 to 150 mm below the distributor tray and openings for the entry of the liquid phase with a diameter of 10 to 25 mm, which are arranged at a height of 40 to 60 mm above the distributor base and openings for the entry of the gaseous phase with a diameter of 5 to 15 mm.
  • the openings for the entry of the liquid phase can be made adjustable in height and orientation.
  • the pressure loss of the gaseous phase between the entry into the reactor and the entry into the spouts via the number and openings for the entry of the gaseous phase is controlled such that at the lowest gas load in the reactor operation, the pressure loss of the gaseous phase between the entry into the Reactor and the entry into the spouts 50 to 500 Pascal, preferably 75 to 300 Pascal, more preferably 100 to 200 Pascal, is.
  • the reactor according to the invention is preferably operated continuously.
  • idler bores are provided in the distributor bottom, which are distributed uniformly over the distributor plate and whose number and size is chosen such that in normal operation of the reactor only a maximum of 5% of the total, passed through the reactor liquid phase flows through the idling holes.
  • the idler holes have a diameter between 10 and 20 mm.
  • the serving as pre-distributor trough distributor having trough-shaped channels with drainage tubes in the trough-shaped channels for the liquid phase is preferably designed such that the trough-shaped channels comprise a main channel and two or more side channels, which are formed so that the liquid phase unhindered between the main channel and the side channels can flow.
  • the main channel and side channels are formed in relation to each other such that the sum of the base area of the main channel and the side channels is 30 to 70%, preferably 40 to 60% of the total cross-sectional area of the reactor.
  • the trough-shaped channels of the trough distributor preferably have a height of from 200 to 600 mm, particularly preferably from 250 to 500 mm, more preferably from 300 to 400 mm.
  • At the bottom of the trough-shaped channels are preferably 30 to 120, more preferably 40 to 100, particularly preferably 50 to 80 openings per m 2 , provided with a diameter of 5 to 40, particularly preferably from 10 to 35, more preferably from 15 to 25 mm , wherein at each opening a drain tube with a diameter of 15 to 75 mm, preferably from 25 to 60 mm, more preferably from 35 to 50 mm is attached, and wherein the length of the drain tubes is set such that the lower end thereof 20 bis 200 mm, preferably 25 to 150 mm above the distributor base.
  • a further improved uniform distribution is achieved by a preferred embodiment of the reactor, after which the introduced via an inlet pipe into the reactor liquid phase at the end of the inlet pipe, at which the liquid phase enters the reactor, and from the end of the inlet pipe by a few centimeters apart a baffle plate in the form of a disc with openings, impinges.
  • the invention also provides a method according to claim 17.
  • the invention also relates to the use of the above-described reactor or of the process described above for carrying out selective hydrogenation of hydrocarbon cuts. Preference is given to a use according to which the hydrocarbon cuts are C2, C3 or C4 hydrocarbon cuts or pyrolysis gases.
  • the hydrocarbon cuts are C4 cuts, with butadiene being hydrogenated from the C4 cuts selectively to n-butenes.
  • FIG. 1 shows the schematic representation of a longitudinal section through a reactor according to the invention R with supply of the liquid phase 1 and the gaseous phase 2 respectively from above, via nozzles, not shown.
  • a mixing and distribution device MV above a fixed catalyst bed F is arranged, which has a trough distributor TV formed Vorverteiler, arranged at the bottom of the same drainage tube A and a distributor base B, which is arranged downstream of the trough distributor TV and acts as a main distributor.
  • spouts T are introduced, which protrude above and below the distributor bottom B into the interior of the reactor R.
  • openings P1 are provided above the liquid level on the distributor bottom B, for the entry of the gaseous phase 2, and openings P2 below the liquid level on the distributor bottom B, for the entry of the liquid phase 1.
  • the trough distributor comprised a main channel and 6 side channels with a height of 400 mm, the sum of the base areas of the main channel and the side channels being 60% of the total cross-sectional area of the reactor.
  • At the bottom of the trough-shaped channels were 62 openings per m 2 , with a diameter of 27 mm, with each opening having a drainage tube with a diameter of 48 mm, and wherein the length of the drainpipes was selected such that the lower end thereof was 150 mm above the distributor bottom.
  • the distributor tray was equipped with 100 spouts per square meter of m 2 , the spouts having a free diameter of 41.9 mm, a length of 320 mm above the distributor tray and 150 mm below the distributor tray.
  • the nozzles each had an opening, 24 mm in diameter, 50 mm above the distributor tray, for liquid phase entry, and a 15 mm diameter aperture near the top of the grommets the entry of the gaseous phase, provided.
  • the mixing and distribution device was charged with water.
  • the water flow rate was varied between 100 m 3 / h and 540 m 3 / h.
  • the mixing and distribution device In the entire load range above, the mixing and distribution device injected only slightly. Through the openings for the gas inlet in the upper area of the spouts no liquid flowed.
  • the mixing and distribution reactor described above was used for the selective hydrogenation of 1,3-butadiene from a C4 cut to n-butenes.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Claims (20)

  1. Réacteur (R) pour la réalisation d'une réaction triphasée d'une phase liquide (1) et d'une phase gazeuse (2) sur un lit fixe catalytique (F), le lit fixe catalytique (F) étant agencé horizontalement dans le réacteur (R), et la phase liquide (1) et la phase gazeuse (2) étant conduites dans le réacteur (R) à co-courant du haut vers le bas par le biais d'un dispositif de mélange et de distribution (MV) en passant sur le lit fixe catalytique (F), le dispositif de mélange et de distribution (MV)
    - comprenant un distributeur à auge (TV) pour la phase liquide (1), muni de canaux en forme d'auge (K) et de tubes d'écoulement (A) dans les canaux en forme d'auge (K) pour la phase liquide (1), et
    - un fond de distributeur (B) placé sous le distributeur à auge (TV), espacé de celui-ci, dans lequel des becs verticaux (T) sont disposés, caractérisé en ce que la longueur des tubes d'écoulement (A) est ajustée de manière à ce que leur extrémité inférieure se situe 20 à 200 mm au-dessus du fond de distributeur (B), et en ce que le distributeur à auge (TV) comprend une ou plusieurs ouvertures (P1) pour l'entrée de la phase gazeuse (2) et une ou plusieurs ouvertures (P2), qui sont placées sous les ouvertures (P1) pour l'entrée de la phase gazeuse, pour l'entrée de la phase liquide (1) dans les becs (T), le nombre et la taille des ouvertures (P2) pour l'entrée de la phase liquide (1) étant configurés de manière à ce que, pour une alimentation de liquide prédéterminée, le niveau de liquide sur le fond de distributeur (B) puisse être ajusté en dessous des ouvertures (P1) pour l'entrée de la phase gazeuse (2) et au-dessus des ouvertures (P2) pour l'entrée de la phase liquide (1), et une tubulure étant placée en amont du fond de distributeur (B), par laquelle la phase gazeuse (2) est introduite dans un espace de tête (G) entre le distributeur sous pression (DV) et un fond de distributeur (B) placé en dessous, espacé de celui-ci, dans lequel des becs verticaux (T) sont disposés, 50 à 200 becs (T) par m2 étant agencés régulièrement sur le fond de distributeur (B) et les becs (T) présentant un diamètre libre de 5 à 75 mm, ainsi qu'une longueur de 100 à 600 mm au-dessus du fond de distributeur (B) et une longueur de 20 à 250 mm en dessous du fond de distributeur (B), les ouvertures (P2) pour l'entrée de la phase liquide (1) présentant un diamètre de 2 à 45 mm et étant placées à une hauteur de 10 à 100 mm au-dessus du fond de distributeur (B), et les ouvertures (P1) pour l'entrée de la phase gazeuse (2) présentant un diamètre de 1 à 30 mm.
  2. Réacteur (R) selon la revendication 1, caractérisé en ce que le nombre et la taille des ouvertures (P2) dans les becs (T) du fond de distributeur (B) pour l'entrée de la phase liquide (1) sont configurés de manière à ce que le niveau de liquide sur le fond de distributeur (B) soit ajusté en dessous des ouvertures (P1) pour l'entrée de la phase gazeuse (2) et au-dessus des ouvertures (P2) pour l'entrée de la phase liquide (1), même en cas de fluctuations de l'alimentation de liquide de jusqu'à 20 % au-dessus et de jusqu'à 50 % en dessous de l'alimentation de liquide prédéterminée.
  3. Réacteur (R) selon la revendication 1 ou 2, caractérisé en ce qu'il présente un diamètre dans la plage allant de 0,5 à 5 m, de préférence dans une plage allant de 1 à 4 m, de manière davantage préférée dans une plage allant de 1,2 à 3 m.
  4. Réacteur (R) selon l'une quelconque des revendications 1 à 3, caractérisé en ce que 70 à 150, de préférence 90 à 130 becs (T) par m2 sont agencés régulièrement sur le fond de distributeur (B).
  5. Réacteur (R) selon la revendication 4, caractérisé en ce que les becs (T) sont agencés selon une distribution triangulaire ou quadratique sur le fond de distributeur (B).
  6. Réacteur (R) selon la revendication 1, caractérisé en ce que les becs (T) présentent un diamètre libre de 10 à 60 mm, ainsi qu'une longueur de 200 à 400 mm au-dessus du fond de distributeur (B) et une longueur de 50 à 200 mm en dessous du fond de distributeur (B), et en ce que les ouvertures (P2) pour l'entrée de la phase liquide (1) présentent un diamètre de 3 à 35 mm et sont placées à une hauteur de 22 à 75 mm au-dessus du fond de distributeur (B), et en ce que les ouvertures (P1) pour l'entrée de la phase gazeuse (2) présentent un diamètre de 5 à 20 mm.
  7. Réacteur (R) selon la revendication 6, caractérisé en ce que les becs (T) présentent un diamètre libre de 35 à 50 mm, ainsi qu'une longueur de 250 à 350 mm au-dessus du fond de distributeur (B) et une longueur de 100 à 150 mm en dessous du fond de distributeur (B), et en ce que les ouvertures (P2) pour l'entrée de la phase liquide (1) présentent un diamètre de 10 à 25 mm et sont placées à une hauteur de 40 à 60 mm au-dessus du fond de distributeur (B), et en ce que les ouvertures (P1) pour l'entrée de la phase gazeuse (2) présentent un diamètre de 7 à 15 mm.
  8. Réacteur (R) selon l'une quelconque des revendications 1 à 7, caractérisé en ce que les ouvertures (P2) pour l'entrée de la phase liquide (1) sont conçues sous une forme ajustable en hauteur et en orientation.
  9. Réacteur (R) selon l'une quelconque des revendications 1 à 8, caractérisé en ce que des orifices de déversement libres sont prévus dans le fond de distributeur (B), qui sont répartis régulièrement sur le fond de distributeur (B) et dont le nombre et la taille sont choisis de manière à ce qu'en fonctionnement normal, seulement au plus 5 % de la totalité de la phase liquide (1) introduite dans le réacteur (R) s'écoule dans les orifices de déversement libres.
  10. Réacteur (R) selon la revendication 9, caractérisé en ce que les orifices de déversement libres présentent un diamètre compris entre 10 et 20 mm.
  11. Réacteur (R) selon l'une quelconque des revendications 1 à 10, caractérisé en ce que le distributeur à auge (TV) est placé 10 à 300 mm, de préférence 20 à 200 mm, au-dessus de l'extrémité supérieure des becs (T).
  12. Réacteur (R) selon l'une quelconque des revendications 1 à 11, caractérisé en ce que les canaux en forme d'auge (K) du distributeur à auge (TV) comprennent un canal principal et deux canaux latéraux ou plus, qui sont conçus de manière à ce que la phase liquide (1) puisse s'écouler sans encombre entre le canal principal et les canaux latéraux.
  13. Réacteur (R) selon l'une quelconque des revendications 1 à 12, caractérisé en ce que la somme des surfaces de base du canal principal et des canaux latéraux est de 30 à 70 %, de préférence 40 à 60 %, de la totalité de la surface de section transversale du réacteur (R).
  14. Réacteur (R) selon l'une quelconque des revendications 1 à 13, caractérisé par une hauteur des canaux en forme d'auge (K) de 200 à 600 mm, de préférence de 250 à 500 mm, de manière davantage préférée de 300 à 400 mm.
  15. Réacteur (R) selon l'une quelconque des revendications 1 à 14, caractérisé en ce que 30 à 120, de préférence 40 à 100, de manière davantage préférée 50 à 80 ouvertures par m2, d'un diamètre de 5 à 40, de préférence de 10 à 35, de manière davantage préférée de 15 à 25 mm, sont prévues au fond des canaux en forme d'auge (K) , et en ce qu'un tube d'écoulement (A) d'un diamètre de 15 à 75 mm, de préférence de 25 à 60 mm, de manière davantage préférée de 35 à 50 mm, est fixé sur chaque ouverture, la longueur des tubes d'écoulement (A) étant ajustée de manière à ce que leur extrémité inférieure se situe 25 à 150 mm au-dessus du fond de distributeur (B).
  16. Réacteur (R) selon l'une quelconque des revendications 1 à 15, caractérisé en ce que la phase liquide (1) est introduite dans le réacteur (R) par le biais d'un tube d'entrée et en ce qu'un déflecteur sous la forme d'un disque muni d'ouvertures est placé à l'extrémité du tube d'entrée, au niveau de laquelle la phase liquide (1) entre dans le réacteur (R), espacé de quelques cm de l'extrémité du tube d'entrée.
  17. Procédé de réalisation d'une réaction triphasée dans un réacteur (R) entre une phase liquide (1) et une phase gazeuse (2) sur un lit fixe catalytique (F), le lit fixe catalytique (F) étant agencé horizontalement dans le réacteur (R), et la phase liquide (1) et la phase gazeuse (2) étant conduites dans le réacteur (R) à co-courant du haut vers le bas par le biais d'un dispositif de mélange et de distribution (MV) en passant sur le lit fixe (F), caractérisé en ce que
    - la phase liquide (1) est introduite depuis l'extérieur du réacteur (R) par le biais d'un tube d'entrée dans un distributeur à auge (TV), muni de canaux en forme d'auge (K) et de tubes d'écoulement (A) dans les canaux en forme d'auge (K), et
    - la phase gazeuse (2) est introduite séparément et/ou avec la phase liquide (1) par le biais d'une tubulure, qui est placée en amont du fond de distributeur (B), dans un espace de tête (G) entre le distributeur à auge (TV) et un fond de distributeur (B) placé en dessous, espacé de celui-ci, dans lequel des becs verticaux (T) sont disposés,
    - la phase liquide (1) étant introduite par le biais des tubes d'écoulement (A) du distributeur à auge (TV) sous le niveau de liquide dans le liquide se trouvant sur le fond de distributeur (B) et
    - la phase gazeuse (2) étant introduite par le biais d'une ou de plusieurs ouvertures (P1) depuis l'espace de tête (G) dans les becs (T) du fond de distributeur (B), et
    - la phase liquide (1) étant introduite par une ou plusieurs ouvertures (P2) en dessous du niveau de liquide du liquide dans les becs (T) sur le fond de distributeur (B) et le mélange de la phase liquide (1) et de la phase gazeuse (2) étant conduit par les becs (T) sur le lit fixe catalytique (F), la longueur des tubes d'écoulement (A) étant ajustée de manière à ce que leur extrémité inférieure se situe 20 à 200 mm au-dessus du fond de distributeur (B), et 50 à 200 becs (T) par m2 étant agencés régulièrement sur le fond de distributeur (B), et les becs (T) présentant un diamètre libre de 5 à 75 mm, ainsi qu'une longueur de 100 à 600 mm au-dessus du fond de distributeur (B) et une longueur de 20 à 250 mm en dessous du fond de distributeur (B), les ouvertures (P2) pour l'entrée de la phase liquide (1) présentant un diamètre de 2 à 45 mm et étant placées à une hauteur de 10 à 100 mm au-dessus du fond de distributeur (B), et les ouvertures (P1) pour l'entrée de la phase gazeuse (2) présentant un diamètre de 1 à 30 mm.
  18. Utilisation du réacteur selon l'une quelconque des revendications 1 à 16 ou du procédé selon la revendication 18 pour la réalisation d'une hydrogénation sélective de coupes d'hydrocarbures.
  19. Utilisation selon la revendication 18, caractérisée en ce que les coupes d'hydrocarbures sont des coupes d'hydrocarbures en C2, C3 ou C4 ou des gaz de pyrolyse.
  20. Utilisation selon la revendication 19, caractérisée en ce que les coupes d'hydrocarbures sont des coupes en C4 et en ce que le butadiène des coupes en C4 est hydrogéné sélectivement en n-butènes.
EP08774160A 2007-06-21 2008-06-20 Réacteur en vue de la réalisation d'une réaction triphasique entre une phase liquide et une phase gazeuse sur un lit fixe de catalyseur Active EP2170494B1 (fr)

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EP3604261A1 (fr) 2018-08-02 2020-02-05 Omv Refining & Marketing Gmbh Procédé de purification d'isobutène d'un flux c4 et installation technique correspondante

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DE102018005694A1 (de) * 2018-07-19 2020-01-23 Linde Aktiengesellschaft Stoff- und/oder Wärmeaustauschkolonne und Verfahren zur Behandlung eines ersten Fluids und eines zweiten Fluids unter Verwendung einer Stoff- und/oder Wärmeaustauschkolonne
EP3604261A1 (fr) 2018-08-02 2020-02-05 Omv Refining & Marketing Gmbh Procédé de purification d'isobutène d'un flux c4 et installation technique correspondante

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JP5276098B2 (ja) 2013-08-28
RU2010101601A (ru) 2011-07-27
TW200916192A (en) 2009-04-16
RU2466784C2 (ru) 2012-11-20
CA2691642A1 (fr) 2008-12-24
EP2170494A1 (fr) 2010-04-07
JP2010530804A (ja) 2010-09-16
CN101778666A (zh) 2010-07-14
CA2691642C (fr) 2015-12-22
BRPI0812907A2 (pt) 2014-12-09
US20100185032A1 (en) 2010-07-22
ATE520455T1 (de) 2011-09-15
KR20100053503A (ko) 2010-05-20
TWI458553B (zh) 2014-11-01
CN101778666B (zh) 2012-10-10
US9011790B2 (en) 2015-04-21
KR101509274B1 (ko) 2015-04-06
WO2008155399A1 (fr) 2008-12-24
MY147674A (en) 2012-12-31

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